Means for handling powdered solids



June 19, 1945. G. w. WATTS MEANS FOR HANDLING POWDERED SOLIDS Filed July 3, 1941 2 Sheets-Sheet l 721 E an 1227222 0 7 Fe erzem lz'on 6259.5; 0

9 4 2 w W h wwo //l/ ll/l/l/l/l/l/ r Z //!//////l///// .9 3 W 75 1 T 4 A w P 5; v I v; G A 4 WI 5 5 3 i 3 s 7 8 MW J 3 M 5 6 m %z a2 k 7 Z 5 J 6 J m n W a a Q g h l u 5 S m 5 E June 19, 1945. G. w. WATTS 2,378,507

MEANS FOR HANDLING POWDERED SOLIDS Filed July 3, 1941 2 Sheets-Sheet 2 n m w wk a g w l. W 1 4 m\ .59 0 a onea i, 6 7 .MJ. 3% 5 7.

aerated. catalyst to Patented June 19, 1945 MEANS F OR HANDLING POWDERED SOLIDS George W. Watts, Flossmoor, 11]., assignmto Standard Oil Gompan tion of Indiana y, Chicago, 111., a corpora- Application July 3, 1941, Serial No. 400,951

(01. zs-zss) 14' Claims.

This invention relates to means for handling powdered solids and it pertains more particularly to improved means for maintaining powdered solids in fluent form and for regulating the downward flow of powdered solids in standpipes, cy-

' clone-separator dip legs, etc.

I The invention is particularly applicable to a powdered or fluid-type catalyst system wherein a powdered catalyst effects conversion while susi is any interruption in this downward flow of separated solids there is a tendency for the solids to bridge and thereby cause a plugging of the conduit. An object of my invention is to provide means for preventing such catalyst bridging or.

p u ing. I

When powdered solids flow downwardly in a conduit and have to be-passed around bends in said conduit the problem of plugging becomes more aggravated. Furthermore such pipe bends are subject to severe erosion. An object of my invention is to avoid such pipe bends insofar as this is possible and to provide'a systemwherein the wdered solids flow downwardly in substantially straight vertical conduits. A further object is to minimize expansion difficulties, particularly during those periods when a powdered catalyst system is being started up or shut down. A further object is to shorten the pipes and conduits required for handling powdered catalyst in a hydrocarbon conversion system and to shorten the structure for supporting such a conversion system. A further object is to avoid the use of the 180 degree bends that have heretofore been used at the base of standpipes for returning a reactor or regenerator chamber.

In order that powdered solids may be handled as a fluid it is essential that such solids be either subjected to mechanical stirring or to aeration, particularly during periods of interrupted flow.

'Powdered solids may flowdownwardly as a fluid there is a tendency for the solids to bridge and cause tube plugging. An object of my invention is to provide means whereby th solids in the standpipe maybe aerated when the flow therein is momentarily stopped.

A further object is to provide improved means for dispersing solids discharged'from the lower end of a substantially straight tube into a hopper reactor or regenerator in which the lower end of the tube terminates. A further object is to provide a new and improved combination of tube closure and agitating or cleaning means in combination with a substantially vertical tube for handling powdered solids. Other objects will be apparent as the detailed description of the invention proceeds.

An important feature of my invention is the provision, at the open downwardly-extending end of a standpipe in a reactor, regenerator or hopper, of an externally operated standpipe closure which is provided with a hollow stem so that steam or other inert gas may be introduced through this closure to efiect aeration when little or no catalyst is being dispersed therefrom,

and so that said steam or inert gas may be used for dispersing catalyst from the base of the standpipe into the reactor or regenerator when substantial amounts of catalyst are flowing from the base. of the standpipe into said-reactor or regenerator.

My improved closure may be of various shapes and designs. It may be provided with a conical tip which will insure centering and with laterally directed orifices or nozzles, communicating with the hollow stem so that the steam or other gases which are introduced through the hollow stem will disperse catalyst into the chamber during the flow of substantial amounts of catalyst and will aerate catalyst in the standpipe during periods of little or no catalyst flow. A vertically movable steam pipe with outwardly directed orifices at its upper end may be slidably mounted within the hollow stem, Mechanically operated stirrers may be secured to and operated by movement of the valve closure.

Another feature of my invention is the provision of means for preventing the plugging of cyclone separator dip legs which extend below the surface of settled solids in a catalyst separation chamber. Variations in pressure or in the level of settled solids in saidchamber may cause the plugging of solids in the cyclone dip legs unless these dip legs are provided with mechanical stirring or aeration means. I have provided'improved closures for said dip legs which may regulate the flow of solids therefrom and I have com- 'bined these closuresawlth a means for main-' taining the catalyst in fluent form in thedit) legs. The means for dispersing solids from these diplegs into,v the settled. catalyst in the hopper .may also serve for aerating the settled solids in the hopper.

The invention will be more clearly understoodlytic cracking and catalyst regeneration system.

illustrating the application of my invention;

Figure 2 is a detail section of one embodiment of a valve closure:

Figure 3 is a detail section of another embodiment of a valve clos Figure 4 is a detail vertical section of a standpipe closure, aerator, and cleaning means; and

Figure 5 is an embodiment of a 'standpipe closure, aerator,.and mechanical stirring means.

While the invention is applicableito a wide variety of catalytic conversion systems it is primarily designed for hydrocarbon conversion processes such as isomerization, desulfurization, polymerization, reforming, isoforming, alkylation, gas reversion, hydrogenation, dehydrogenation,

, etc. and it is particularly'applicable to the catalytic cracking of gas oils and heavier hydrocarbons.

The charging stock may consistof or. may con tain hydrocarbonsproduced by other conversion processes such as cracking or coking, hydrocarbons synthetically produced by the hydrogenation of carbonaceous 'materials, or hydrocarbons produced by a carbon monoxide hydrogen synthesis.

In my preierred embodiment I will describe thc invention as applied to the catalytic cracking of Mid-Continent gas oil.

The gas. oil feed stock is vaporized and heated 1 in conventional'heat exchangers in pipe still coils to a temperature of about 800 to 1000 F. for example about 900 F.,' and is introduced at a pressure 'of about atmospheric to 50 pounds per square inch, for example about pounds per square in'ch,, through transfer line 10 to the bottom of rea actor 'I i. Various amounts of steam may beincluded with the hot vapors so introduced.

When it is .desired to subject these vapors to partially spent catalyst before they are contacted with fresh catalyst such partially spent catalyst may be dispersed into th vaporized hydrocarbcms from the bottom of standpipe II. The amount 0! catalyst so introduced may be controlled by raising or lowering closure member l3 which is supported by hollow shaft l4 extending through packing gland l5 and externally raised or lowered by means of valve handle 16 or by any other manually or automatically operated mechanism known to those skilled in the art. Steam or other inert gas is introduced into the hollow stem I! through line I! in amounts controlled by valve it. The hollow stem terminates in laterally the catalyst is maintainedin fluent or'liquid-like condition in the standpipe by means of aeration ga's which is introduced through inclined ports [9 adjacent the periphery of the standplpe. For ae'ration the vertical velocity of the steam or aerating gas in the-standpipe should usually be about .05 to about .5 foot per second but this will, of course, depend upon the nature of the catalyst,

its fineness, density, etc;

' The conical closur 'is self-centering and the hollow stem I4 is sufficiently flexible-to permit a fairly-tight seal regardless of any slight movement at the base of standpipe l2. or any slight movement ofclosure member it while it is in the open position.

Various modifications in the size and shape of the closure member may be made without departing from my invention. For example, I may employ a substantially flat closure 20 as shown in Figure 3 ,and the lateral ports l9 may beso directed as to sweep this surface free of catalyst so that 'when the closure approaches the end of standpipe l2 a cleaner and tighter seal may be obtained than would otherwise be possible. The valve seats may be so positioned as to prevent any scouring or erosion thereof, the lower seat bein protected by the aerating gas screen and the upper being out of the direct path of catalyst flow. Fresh, or regenerated catalyst may be introduced into the reactor through standpipe 2| in amounts regulated by pipe closure 22 which is directed ports or nozzles 19 (see Figure 2) the gas supported by hollow stem 23 extending through packing gland 24 and externally operated by a manual or automatic control mechanism 25. Steam is introduced to hollow shaft 23 through line 26 in amounts regulated by valve 21.

The reactor l I should be of such size and shape as to effect contact of the vapors with the necessary amount of catalyst and for the necessary amount of time. In this case the catalyst is preferably of the silica-alumina or silica-magnesia type and it may be prepared by the acid treatin of natural clays such as bentonite or by synthetically preparing a, powdered silica-alumina or silica-magnesia mixture. Such a mixture may be prepared by ball-milling silica hydrogel with alumina or magnesia, drying the resulting dough at a temperature of about 240 Fsand then activating by heating to a temperature of about 900 to 1000 F. The catalyst per se forms no part of the present invention audit is, therefore, unnecessary to describe it in further detail.

With catalyst in powdered form, having a particle size of about 10 to 100 microns, I prefer to employ vapor velocities in the reactor of about .4 to 4 feet per second, for example about 1 /2 or 2 feet per second in the reactor. The catalystto-oil weight ratio may be about 1:1 to about 8:1 and is preferably about 4:1. The catalyst residence time may range from a few seconds to an hour'or more but is preferably about 5 to 10 minutes. The vapor residence time is usually about 10 to 30 seconds. The catalyst introduced through 1ine,2l is preferably at a temperature of about 900 to 1000 F., for example about 950 F.,

and the temperature prevailing throughout the geactor may thus be maintained at about 900 to Reaction products and suspended catalyst pass from the top of the reactor through pipe 28 into enlarged settling chamber 29 which may be providcd with a baflle 30 for distributing the suspended catalyst stream uniformly in the settling chamber thus preventing a chimneying effect. Cyclone separators may be employed in the top as'ra o'ot" introducethe recycled catalyst at-a higher point of the settling chamber for-removing catalyst which has failed to separate out inv the separatingchamber. The products which are thus substantially freed from catalyst are withdrawn through line 3| to a product fractionation system (not shown) wherein a gas fractiona gasoline fraction and one or more gas oilrractions are separated from each other by any conventional means known to -the art. Any remaining traces of catalyst maybe recycled with the heaviest fraction back to the initial heating step with fresh feed. The settled catalyst'in chamber 29 is main-- tained in fluent condition by the introduction of I 5 900 F. and the regenerated catalyst at a temperature about 850 F. but it will be understood that. these temperatures may be varied within in the regenerator than the point at which spent catalyst is introduced thereto. The spent catalyst may be introduced at a temperature of about wide-limits- Since the reactor may be about feet or more in; height and'the regenerator may be even higher, it is obvious that provision must be made to take care or differential expansion during the starting up or shutting down of the system. This an aerating gas such as stem through distribut- 1 ing means 32', the steam serving to strip the hydrocarbon vapors from the catalyst as well as packing gland 38 to external operating means.

Steam is introducedinto the hollow stem through line 40 in amounts controlled by valve 4| and this steam disperses the catalyst into the incoming,

air in the manner hereinabove described.

The gas velocities in the regenerator may'be substantially the same as in the reactor and sufficient time is allowed in the regenerator to permit the combustion of carbonaceous material from .the catalyst. Regenerated catalyst is carried from the top of the regenerator by the regeneration gases through pipe 42 into enlarged Y settling chamber 43 and the gases are distributed -in this settling chamber by means of baflle 44.

Hereagaincyclone separators may be employed for removing further amounts of regenerated I catalyst from .regeneration gases and the final residue of catalyst may be separated from said asesjin-anelectrostatic precipitator. The 'hot from this part of the system. This heat extraction may be effected by recycling a substantial part of settled catalyst from chamber 43 through line 48, heat exchanger 41 and pipe 48 back to the regenerator tower 34. I prefer to pass the. catalyst through tubes in this heat exchanger and to introduce a cooling fluid around the tubes. through line49 to withdraw said fluid through line 50.

The amount heat exchanger may be regulated by the position of closure member 5| which is supported by hollow stem 52 extending through packing gland 53 to externally operated control means 54. steam is introduced into the hollow stem through line 55 in amounts regulated by valve 58.

The temperature of the recycled catalyst may be controlled by regulating the amount and temperature of the cooling fluid or by regulating the amount of recycled catalyst, or both. I prefer to of catalyst recycled through the problem is greatly simplifled by the use 01' the relatively short substantially straight standpipes which may be employed with my improved standpipe closure and aerating mean hereinabove described. Simple expansion joints 51 are provided in standpipes 2| and 33.

As above stated, cyclone separators may be employed in settling chambers 29 and 43 for removing residual catalyst particles from the gases which are discharged therefrom through lines 3| and respectively. These cyclones are preferably mounted inside the chamber and around the periphery thereof and may be connected in series or in parallel or both in series and in parallel.

--I have illustrated primary cyclines 58 and secondary cyclones 59, but any number of stages may be v.,used. All of these cyclones are provided with dip legs 6|) which may be either concentrically or eccentrically mounted in order that they may be positioned adjacent the outer chamber walls and may extend vertically to a point adjacent the outwardly extending chamber bottom 6 Gases from the upper part of the chamber are introduced through openin s 52 into the primary cyclones. Gases are conducted from the primary to the secondary cyclones through lines 63 and gases are removed from the secondary cyclones through lines 54 to line 3|.

With a pressureof about 8 pounds in thesettling chamber, the pressure in the primary cyclones may be about 7 /2 pounds and in secondary cyclones may be about 7 pounds, this difference in pressure being balanced by the head of separated catalyst in the respective dip legs 60. If for any reason there is a surge in pressure in chamber 29'or'an increase in the height of the level of settled catalyst therein, the downward flow of catalyst in dip legs 60 may temporarily cease and thuspe'rmit compacting and bridging of catalyst in these dip legs. When the dip legs become plugged with deposited solids in this manner the cyclones are rendered inoperative'and a feature of my invention is the provision of means for preventing the pluggingof these dip legs and for cleaning the dip legs if they do become plugged.

Catalyst dip legs 30 are intact small stand.-

pipes and I may provide closures for .the bot-' tom of thesestandpipes similar to the standpipe closures already described. Beneath each dip leg I may provide a closure member 66 which is mounted on a hollow stem 51 extending through a stufllng box 68 to external control means 59. In Figure 4 I have illustrated an arrangement in which the hollow stem 51 is slidably mounted in conduit III which carries a yoke 1| with a bearing 12 in the lower arm thereof. In this bearing a threaded member I3 may be rotated by wheel or lever 69 for moving closure 68 toward and away 'from the lower end of dip leg 60. In this particular modification a separate steam pipe 14 is slidably 4 v mounted in the hollow valve stem and provided 4 with laterally directed ports II at its upper end. The lower end of this pipe is connected to steam line 18 so that the steam introduced in regulated 'amounts through line ll is dis- By means of 11 (or by other suitable means) tube It may be raised or lowered without changing the-position of closure mem ber 86. Thus if there should be any plugging I or accumulations ofsolids in standpipe or dip 'leg 60 the .inner pipe 14 may be advanced "throughout the entire length of the dip leg and any accumulated catalyst particles may be blasted from the inner walls of the dip legs by steam from ports 15. Thus steam from these ports may serve three distinct functions: (1)it.

may serve to effect aeration in the standpipe, (2) it may serve to discharge catalyst from the base iii the standpipe, and (3) it may serve to scour the standpipe and free it from any deposits or catalyst particles.

] Ini'igure 5 I- have shown another modification or my invention wherein closure member '"66' is supported by hollow stem 61 but is rotat- "ably mounted around aninner pipe 18. In this case it is the inner'pipe which is raised or lowered by valve closure means 89 and the valve closure itself may be rotated by means of a suitable wheel or handle 19. The aeration ports in this case may be provided in the valve closure asiIIustrated in Figure 2. Secured to the'top oi the valve closure in -this modification is, a rod I0 with stirring vanes Q I secured thereto, thus a stirrer'is provided for the catalyst in standpipe 6|) which'can be used for dislodging any bridged catalyst material and for maintaining the catalyst in fluent form in tube 60. This stirrer may 'bemoved vertically to. an extent sumcient to permit vanes 8| to traverse the entire space within the tube and by rotating or raising and lowering this stirrer or by simulment with the open end oi. the standpipe. Instead of introducing steam below the valve operating means I may provide a steam Jacket around the valve stem below stufling box 88 and above the handle or valve regulating means. The aeration-gas or steam line may be connected directly to this steam jacket, the .upper and lower ends of the steam Jacket may be closed by suitable stufllng boxes in order to permit rotation and vertical movement of the hollow valve. stem therein, and one or more holes may be drilled in that portion of the valve stem which is within the steam jacket to provide communication between the steam iacket and the hollow interior of the valve stem. These and equivalent structures are all included within the ,scope of my invention.

The hollow valve stem, particularly of the type illustrated in Figure 4, provides access for the introduction of boring tools or plungers for cleaning the dip leg orstandpipe. It will be seen that tubularmember I4 may be completely withdrawn from hollow stem 81 and that any suitable reamer, scraper or other tool may be inserted through hollow valve stem '1. The tool may contain means for aerating as well as for boring the dip leg. v r I I claim:

1. In a system for handling powdered solids, a chamber for contacting suspended solids with gases or vapors, a conduit extending downwardly into said chamber, means tor introducing powdered solids into the conduit at its upper end and for maintaining a pressure head at its lower end greater than the pressure in the chamber at the lower end of the conduit a closure for said conduit, a hollow stem supporting said closure and extending to a point outside of said chamber, means outside of said chamber for moving said closure with respect to the end of said conduit.

.saidclosure having an orifice communicating with the opening in said hollow. stem and means taneously rotating'and moving the stirrer in a vertical plane I may maintain the desired operation of the standpipe without any interruption; Steam may be introduced through line 82 in for introducing a gas through said hollow stem and said orifice for aerating powdwrnaterial in said conduit when saidiclosure is in closed position.

2. The system defined byelamkrwiierem the orifice is laterally incurred and whereby solids are dispersedi'rom said conduit into said chamber when said closure is in open position.

3. The system 01' claim 1 wherein said closure is provided with a conical portion for centering said closure with respect to said conduit.

4. In a fluid-type catalyst systemof the type wherein Powdered catalyst effects conversion while suspended in hydrocarbon vapors in a conversion reactor, is then separated from the hyfluent form. While I have illustrated. certain examples of pneumatic and mechanical devices for maintaining solids in a fluent condition in vertical 'standp'ipes itshould'be understood that my invention is not limited toany 'of these particular examples sinc various other modifications of the invention will be apparent to those skilled in the art from the above description. The invention is not limited to the conical upper surface of the valve for positioning or centering the valve and it should beiunderstood'that a suitable yoke or guide means may be secured to the lower part of any standpipe for maintaining the closure member in aligndrocarbon vapors and suspended in a, ga for regeneration ina regenerator reactor and is finally separated from regeneration gas and returned for further conversion, the apparatus which comprises a large vertical reactor, 5 conduitextending downwardly in said reactor, a closure for said-conduit inside .of said reactor, a hollow stem for said'closure extending to a point outsideof said reactor, means outside or said reactor for controlling the position of said closure, at least one orifice in said closure communicating-with said hollow stem and means for introducing steam through-said hollow stem for aerating catalyst in said conduit when the closure is in closed position and for dispersing catalyst insaid reactor when the closure is in open position.

5. In a system for handling finely divided solaavaeov ids. a large chamber. a substantially vertical standpipe extending downwardly in said chamher. a .closure member mounted beneath said standpipe on a hollow stem extending through said chamber wall, means outside of said chamber for regulating the position of said "closure member, means for introducing an aerating fluid through said hollow stem and means supported by said hollow stem for dislodging deposited solids from said standpipes.

6. The apparatus of claim 5 wherein the means for dislodging solid particles comprises a tube slidably mounted within said hollow stem, said tube being closed at its upper end and being provided with outwardly directed ports for directin a fluid against the standpipe walls when the pipe is raised or lowered.

7. The apparatus of claim 5 wherein means for removing deposited solids comprises a mechanical stirrer secured to the closure member.

8. In apparatus for removing finely divided solids from gases an enlarged separating chamber having outwardly extending bottom wall, means for retaining a layer of separated solids in the lower part of said chamber, a cyclone separator mounted at the periphery of said chamber, a dip leg extended from said cyclone separator to a point beneath the layer of separated solids in said chamber and above the outwardly extending bottom wall, a closure member mounted underneath the end of said dip leg and supported by a hollow stem extending through said outwardly extending bottom wall, means outside of said chamber .i'or regulating the position of said closure memend of the standlilli means for introducing an aerating gas through said hollow support and Ill said closure member into downwardly flowing catalyst powder, and means for centering said closure member with respect to the lower end of thestandpipe.

10. The apparatus of claim 9 which includes means for introducing a cleaning tool through said hollow supporting member and into said standpipe.

11. The apparatus of claim 9' which includes means for introducing a cleaning tool through said hollow supporting member into said standpipe and means for introducing a gas into said standpip through said tool.

12. In catalytic conversion apparatus a vertical reaction chamber, an enlarged catalyst sepavration chamber above said reaction chamber with a laterally inclined wall connecting the separation chamber to the reaction chamber, a cyclone separator mounted in said separation chamber at the periphery thereof and provided with a downwardly extending dip leg terminating above the outwardly extending wall, a closure member for the bottom of said dip leg, a hollow support for said closure member extending downwardly at'the bottom of said standpipe, a hollow support for said closure member extending through the chamber wall, means outside or the chamber wall for raising and lowering said closure member toward and away from the lower end of the standpipe and means for directing gases item the hollow support through the upper part oi the closure member while said member is in closed position.

14. The apparatus of claim 13 wherein the clo sure consists of a central conical surface and a lateral valve seating suriace..

GEORGE W. WA'I'IS. 

